Catalytic conversion of hydrocarbons



Dec. 26, 1944. P. MATHER Erm. 2,365,893

CATAYTIC CONVERSION OF HYDROCARBONS Filed Aug. 5,1939 2 Sheets-Sheet'l INVENToRs PERCY MATl-jl-:R

LEV A. MEKLER @256M/EMV y ATTORNEY 3 8. S. me E o mm O, wm Uv mm :WAV m m z A A u nu mumzmnzo o nm mm 0 m f T N q nv v mm mm N 3N. v -d E. i

mmmzmn zouV cv vv .ma .v mm t 2212; E mv. E...

A. ma Nu ,u

Dec. 26,A 1944; p MATHER TAL 2,365,893

I CATALYTIC CONVERSION OF HYDROCARBONS Filed Aug. 5, 1939 2 sheets-sheet 2 HIAFPETA/A/Le By- PA ss P/Pfs INVENTORS Plv-:Rev MA1-HER LEV A. MEKLER l f Y y f TORNEY I thro i dium is circulated during processing oi' the re- Patented Dec: 26., i

FFIC

oA'rAL'YrIc .ooNvansloN or Percy Mather and Lev A. Meklei', Chicago, mit,J assignors to Universal Dil Products 6cm,

Chicago, Ill., a corporation ot Delaware Y applicants august s, iosa sei No esatto i5 olaf (oi. its) The invention iis more specifically directed to an improved process involving simultaneously conducted endothermic and exothermic reactions..

Hydrocarbons are converted in the endothermic step oy passing the same in heated state in oontact with a bed of catalytic material which proa motes the desired conversion reaction and, in the exothermic step, heavy carbonaceous conversion products deposited on the catalyst particles dun ing the endothermic step are burned therefrom to renew the activity of the catalyst by passing a stream of hot oxygen-containing gases through the catalyst bed. v

In many of the processes oi commercial signicance so far developed for the catalytic conversion' of hydrocarbons into products' of a more valuable nature, the formation and deposition of hydrocarbonaceous materials in the catalystbed progresses-at such a rate that frequent reactivation of the' catalyst isrequired. It is, there-` fore, expedient for accomplishing this reactivation in situ, (i. e., Without removing the bed of catalytic material from the reactor whereirrit is disposed and employed to promote the endothermic reaction) In order to operate continuously and avoid interruption of the desired reactions, it is likewise common practice to employ a plurality ofreactors, each containing one or more lbeds of the catalytic material,.with provision for alternating the reactors with respect to the endothermic and. exothermic reactions, one or more of said reactors serving as .the zone in which conversion of the hydrocarbons' is accomplished while the catalytic material in one or more reactors is being reactivated.' I A l f The 'common expedient for Ysupplying the -rev-quired heat to the catalyst bed and hydrocarbons undergoing conversion in the endothermic step is to jacket the reactor or provide tubular elements or the-like withinthe catalyst bed, through which jacket or tubular elements a relatively hot con. vective medium is vpassed in indirect heat ex,. change with the 'catalyst and Vthe reactants.'

the catalyst, to accomplish its .reactivation is an exothermic reaction which requires control to prevent excessive heating of the catalyst bed vand consequent possible destruction of the catalyst or permanent impairment of its Since burning of the carbonaceous deposits from catalytic activity,

the same jacket, tubular 'elements or the like.-

h whiclrthe .relatively hot convective ineactanta is ordinarily employed for circulatinga transfer reiaoon'withthe cstaiyst, @manine gases reactivation. v I

Since relatively large quantities oi heat are ordinarily evolved in the exothermic step, it is necessary, for good thermal emciency., to recover a substantial portion of the available heat in the spent reactivating eases ior some useful pur and the hot combustion products formed dg r pose. in many instances. this available heat will v fulfill a, maior portion, of the heatrequirements 'of the endothermic step and its use for this pur= pose makes for greater economy anda more seite contained bprocess. This has been accomplishedl in previous systems of this general type by ein` Aplaying the same convective medium for heating in the endothermic step and for cooling in the` exothermic step, the conductive medium heine i circulated, rst in indirect heat transfer relae tion with the catalyst in the reactor wherein reactivation is taking place and then in indirect heat transfer relation with the catalyst in the.. reactor wherein processing or conversion oi' the hydrocarbonsistaking place. .v *.The present invention follows the conventional practicel with respectv to periodic processing of the reactants and reactivation of they catalyst in-situ. but involves a decided and advantageousgde'j parture from prior practice with respect tothe method provided for transferring heat from the exothermic tothe endothermic reaction and conj trolling temperatures in both the endothermic and exothermic steps. u 'To maintain the hydrocarbonireactants within the temperature range at whiclrtheir desired con- '35 version'will progress satisfactorily during their contact with the catalyst, we employ a plurality of catalyst beds through whichv the reactants are passed in series and heat the reactants priorl to their contact with each catalyst bed. The V#size of each catalyst bed and the consequent degree of conversion obtained tlerein is so regulated that the temperature of the-reactantsgas they are cooled by the heat given--up to the endothermicv reaction as they pass through the bed, is not re-f duced to belowv theoptimum range' within the catalyst bed. The heat thus lost by the reactants is replaced and the desired higher temperature levelvreestablished as the reactants pass from each catalystl bed of the series to the next successive bed by reheating 'the reactants between tering each catalyst bed does not exceed the opu timum range for accomplishing the desired conv lrelatively cool convective medium in indirect heat lversion therein. It is within the scope of the iri-A vention to employ substantially the same range of temperature within each. of the several catalyst l beds or to vary the temperatures with respect to the several beds to suit requirements. For example, progressively increasing or progressively decreasing average temperatures may be employed in the successive catalyst beds or conditions may be regulated to establish a vpredetermined maximum or minimum average temerature at an intermediate point in the series of eds.

To transfer the exothermic to the endothermic step, we employ masses of refractory material such as cerl,amies or metals of relatively high heat capacity through which the hot reactivating gases are passed following contact-l thereof with the catasubstantial quantities of heat from' lytic material being reactivated, whereby heat is given up from the hot reactivating gases to the refractory mass and stored therein. When the reactor containing the thus heated mass of refractory material is changedover from reactivating to processing service, the reactants to be converted are passed through the mass of hot refractory material vprior :to their contact with the catalyst bed in this reactor and a portion ofthe heat required for conducting the exothermic reaction is thereby imparted from said heated mass to the reactants by direct contact therebetween.

The endothermic and exothermic steps .are seldom in exact thermal balance; i. e., the heat which can be transferred from the exothermic to the endothermic step will not 'exactly correspond to the heat requirements of the endothermic step. The invention, therefore, provides for further adjusting the temperature-of either the reactants or the reactivating gases, or 'both,prior to each contact thereof with the successive beds of catalytic material, in addition to the adjustment accomplished 'by contacting these materials with the refractory material disposed between the successive catalyst beds. This may involve either further heating or partial cooling ofthe reactants and/or either further cooling or partial reheating of the reactivating gases and adjust- I ment of the temperature of the reactants and/or reactivating gases in either direction is within 4the scope of the invention. In the instances most material and stored therein for subsequent use Many of the features of the invention herein disclosed, including the improved -form of reactors provided and the methods above outlined of transferring heat from the exothermic to the endothermic reaction and controlling reaction temperatures in both the endothermic and exothermic steps, may be employed to advantage in a wide variety of processes involving simultaneously conducted endothermic and exothermic reactions wherein the endothermic reaction is catalyticallyv promoted and the exothermic reaction comprises reactivation of the catalyst. Catalytic cracking, dehydrogenation, aromatization and cyclization are afew well known examples of such processes to which the features of the invention, above mentioned, areapplicable. However, in someof its more specific aspects the invention herein provided and claimed is particularly directed to catalytic cracking and since a more detailed description of this phase of the invention will serve as a specific illustration of the features and advantages of the invention, we have selected a catalytic cracking system for illustration in the accompanying Adiagrammatic drawings and the description of the drawings is directed to a description oi the system and its operation for catalytically cracking hydrocarbon oils.

Fig. 1 of the drawings is essentially a flow diagram of thecatalytic cracking system employing the features provided by the invention and Fig. 2

illustrates one specific form of reactor embodying certain features of the invention and which may be employed to advantage with `the process flow illustrated in Fig. 1.

Referring to Fig. 1, the raw oil charging stock is supplied through line I and valve 2 to pump 3 by means of which it is fed through line 4 and valve 5 into fractionator 6, wherein it directly commingles with the vaporous conversion products undergoing fractionation, is heated by contact with the vapors and serves to assist their fractionation. The thus preheated charging stock commingled with reflux condensate, comprising heavy fractions of the vaporous converf sion'products which are condensed in fractionator 8, is removed as combined feed from the lower portion of the fractionator, wherein it accumulates, and isdirected through line 'I and valve 8 to pump 9, by means of which it is fed vthrough line I0 and valve II to heat exchanger I2.v

It passes through heat exchanger II inindirect contact with the hot conversion products priorv to their fractionation. The resulting preheated combined feed is directed from heat exchanger I2 through line I3 and valve to heater I5.

The function of heater I 5 is to supply sufficient heat to the combined feed to effect its substantiallyf' complete vaporization at -therequired during processing of the reactants, independent oi' the heat, available for this purpose in theA hot reactivating gases. It alsoprovides for maintaining the quantity of heat supplied from the refractory material tothe reactants and maintaining .the temperature at which the reactants are supplied to the catalyst bed substantially uniform during the entire processing period in each reactor regardless of the reduction in the temperatu'e of the refractory mass, as the period progresses, due to the heat supplied therefrom to the reactants. The method whereby these con- -trols are obtained, will be described in conjunction. with the accompanyingv drawings. l

superatmosphenic pressure and any desired form of heater capable of accomplishing this may be employed within the scope of the invention. Whendesired, in order to reduce the eifective pressure, assist vaporization and aid in preventing substantial thermal decomposition of the oil, regulated quantities of relatively inert, low molecular weight material such as steam or hydrocarbon gas may be commingled with the combined feed prior to its introduction into heater I5. Line II and valve I1, communicating with line I3, is provided for this purpose in the case here illustrated. The highly heated and .substantially vaporized combined reed is directed from heater ls through line I8 and valve I9 t'o a separator or'knock-out drum 20, which may be empty, provided with aseases bailes, perforated pans or the like or it--may contain tar-absorbing or polymerizing materials, wherein any high coke-forming unvaporized fractions of the combinedfeed are separated from therelatively clean vapors, the latter being di rected from drum 20` through line 2| to the .catalytic reactors, as will be later described, while the non-vaporous high coke forming materials are removed from drum 20 and from the system through line 22 and valve 23 or permitted to de posit on the material within the drum and periodically removed byburning the, deposited'high coke-forming materials from the absorbent mass same temperature as that of the reactantsenteror replacing the mass withlfresh absorbent ma-v terial. v In the particular case here illustrated, two sets or groups, A and B, oi catalytic reactors are emf ployed, group A 'consisting of three reactors Ai, A2 and A3 and group B consisting of'three reactors BI, B2 and B3, the reactors oi each group being connectedln series and the two groups being connected in'parallel. it is, oi course, with.

in the scope of the invention to provide any desirednumber of reactors in each group; Preferably, the reactors are substantially identicaland may be oi' the general'form illustrated in Fig. 2

and hereinafter described or oi any other suitable form capable of accomplishing the same purpose.

In this'v particular instance, each of the reactorscontains asingle bed of catalytic material capable of promoting the cracking reaction and of su- 'ciently small volume in relation to the quantity of vaporous hydrocarbon reactants passed therethrough in a given time that the temperature drop through each catalyst bed will not be excessivel (i. e., the temperatures prevailing throughout the catalyst beds `are within the optimum range for converting the reactants into high yields oi good antiknock gasoline).

Each of the reactors also contains a bed ormass pacity or metal whichis not adverselyv affected by and does notvadversely affect thereactants or the catalyst. vThe vaporous .hydrocarbon reactants are passed through this mass and heated by contact therewith to the desired conversion temperature prior to their contact with the catalyst.

beds andlthe beds of. refractory material may be disposedv in separate structures lwith arrange.- ment for the series ow of reactants iirst through a bed of refractory material then through acatalyst bed throughout the series.

-Eajch group of lreactors is alternately employed for processingthe reactants and for reactivation of the catalyst. theI refractory material in the Areactors of the group in which thecatalyst lis of refractory material oi relatively high heat ca- `bed of the latter on the up-str'eam vside oi' theiirst catalyst bed or, when desiredthe catalyst being reactivated being heated by the hot reacti-fv` vating gases issuing from the catalyst beds and' the refractory material thus heated during reactivation being subsequently employed in these `reactors during processing to supply heat `to -the reactants prior to their contact with the catalystV in each reactor.

When the reactors of group A are employed for ing reactor Ai. The thus reheated reactants pass from heater Cl through line 32 and valve 34 into reactor A2 wherein further cracking is accomplished in the same manner as in reactor AI. The resulting partially cooled reactants pass through line 36 and valve 33 to heater C2, wherein their temperature is again increased, as desired, and wherefrom the reheated materials pass through line it and valve d2 into reactor At. The cracking reaction is completed in reactor At in the same manner as described withreference to reactors Ai and A2. The resulting conversion products, which are still at a relatively high temperature but somewhat cooler than the stream supplied to reactor A3, are directed from the lat- -ter zone through line llt, valve it and. line t8 to heat exchanger i2, 'wherein their temperature is substantially further reduced by indirect heat exchange with the combined feed passed through this zone, as previously described, and where from the conversion products pass through line t9 and valve til to the vaporizing and separating chamber El. v

Before the formation and deposition of heavy carbonaceous materials on the catalyst particles has reduced the activity of the catalyst in the reactors of group A to a point where excessive degradation in the yield and quality of products would result, the stream of vaporousreactants is divertedfrom the reactors of group A andsupplied through line 25 and valve 2li to the reactors of group B, wherein the cracking reaction continues while the catalytic material in the reactors of group A is reactivated, as will be subsequently described. y

In each of the reactors of group B, conversion and 'heating of the reactants is accomplished in the same manner as previously described with reference to the reactors of group A, heaters Ci Y ,and CI performing the same functioxras heaters "C I and C2, the flow of reactants being from reactor Bl through line 29 and valve 3i to heater C3, thence through line 38 and valve 85 to reactor B2, thence'through line 3T and valve t!)` to heater C4. thence through line M and valve 43 to reactorBS, the conversion products naly passing from reactor B3 through line, valve ll'lv and line 48' to heat exchanger I2 wherefrom 'the partially cooled conversion productsl are'y dif rected through line 49 and valve 50 to the vaof the iracu represented as tubular heat -exchangers through which a convective medium, such as combustion -gases or a liquid or vaporous'medium vsuch asa suitable salt, eutectic' mixture of salts or low melt-l at the required temperature in indirect .heat transfer relation with4 the reactants. When desired, any other suitable form of heater such as a' furnace having a closed coil heated by combustion products generated. within the furnace strueture may be employed within the scope of the invention, but ordinarily this form of structure is not `preferred since it is capable of functioningA eihcientiy as a heater only, while a heat exchanger may be employed to transfer heat in either direction. This is important since, although referred to as heaters, members Cl to C4 inclusive, in the case here illustrated, function as coolers for the stream of revivifying gases, fas will lbe later explained, when the catalyst beds in the reactors to which they are connected are being reactivated. This ohviates the use of separate heating and cooling facilities between the reactors.

The conversion products supplied, as previously described, from the group of reactors in which processing is taking place to separating chamber' 5| are therein separated into relatively clean vapors and residual liquid components. ,The latter are removed from the lower portion of chamber 5| through line 52 and valve 53 to cooling and storage or elsewhere, as desired. A- suitable pump, not shown, may .be employed when required for removing residual liquid from chamber 5| and directing it to the desired destination.

The relatively clean vapors from chamber 5| are fractionated in the upper section of the same column, designated as fractionator 8, in commingled state with the charge, to condense as reflux condensate their components boiling above the range of the desired final products. 'I'he fractionated vapors of the desiredend-boiling point are directed from the upper portion of fractionator 6 through line 54 and valve 55 to condenser 56 wherefrom the resulting distillate and -uncoh I densed gases are directed through line 81 and valve 5 8 to collection and separation in receiver 59. Y Since the process is preferably operated at rel-f atively low superatmospheric pressure, consider- 4 able quantities of low-boiling, normally liquid fractions will usually be included in .the normally gaseous fractions collected in receiver 59. These materials are directed from the receiver through line 88 and valve 8|, preferably to suitable absorption equipment of any desired conventional form, not illustrated. capable of recovering the desired heavy fractions from the gases.

The distillate collected in receiver 59 will contain substantial quantities of dissolved normally gaseous fractions and is directed from the receiver through line 82, valve 83, pump 84, line Il, valve 66, heat exchanger 81, line 88 and valve 89 to stabilizer 18, wherein regulated. quantities of the dissolved gases are liberated to obtain a final liquid product of the desired vapor pressure.-

Preferably, regulated quantities cf the` distillate collected in receiver I8 are returned therefrom by well known means, not illustrated, to

the upper portion of fractionator l -to' serve as a 65' cooling and reiluxing medium in this zone.

The distillate to be stabilized is reheated in passing through heat exchanger; 81 by indirect heat exchange with the reboiled bottoms4 from the stabilizer, reboiling being accomplished, in the case here illustrated, by directing regulated quantities of the combined feed from fractionator 8. through line 1| and valve 12 to pump 13 wherefrom it is supplied through line 14 and valve 18 to reboilerl 19, passing therethrough in indirect heat exchange relation with bottoms from stabi llzer 18 which are supplied to the reboiler through line 11 and valve 18. The vapors evolved in reboiler 16 are directed therefrom through lines 19 to the stabilizing column and the resulting cooled combined feed is returned from the reboiler through'line 80 and valve 8| to fractionator. 5. The hot reboiled distillate comprising the hnal light liquid product of the desired vapor pressure is directed from the reboiler through line 82 and valve 83 toheat exchanger 81, wherein it suppilesfheat to the distillate passing to the stabilizer by indirect heat exchange therewith, the final stabilizedproduct being directed from heat exchanger 81 through line 84 and valve 85 to further cooling and storage or elsewhere, as desired. y

The gases evolved from the distillate in stabilizer 18 are directed Iromthe upper portion thereof through line 88 and valve 81 to cooler 88, wherein they are partially condensed to form a reiluxing medium for use in the stabilizing column, the resulting normally gaseous con- -densate and uncondensed gases passing from cooler 88 through line 89 and valve 90 to accumulator 9| wherei'rom condensate is returned by means of line 92, valve 93, pump 94, line 95 and valve 96 to the upper portion of the stabilizer as a cooling andreiluxing medium, while the gas is released from the accumulator through line 91 and valve 98 lto storage or elsewhere, as desired.

' erated. gases, after mixing in the generator with cooler combustion gases supplied thereto as hereinafter described, are directed through line |85 wherefrom they are supplied through valve |38 toA thereactors of group A, when regeneration is taking place in the latter, and through line |81 5 and valve |38 to the reactors of group B, when they are being employed for regeneration.

'Ihe general direction of ilow through each re# actor and through the series of reactors during regeneration is in the lcase here illustrated redesired degree.

verse to the i'low therethrough during processing. When the reactors of' group A are employed as catalyst regenerating zones,.the hot combustion gases with which regulated quantities of air are commingled, by introducing the latter intov line |35 through line |48 and. valve |4|, pass into reactor A8 wherein they contact the catalyst .mass disposed therein and burn depo sited carbonaceous material therefrom. whereby the temperature ofthel reactivating gases is materially increased. They then pass through the mass of refractory material disposed in this reactor and give up a substantial portion of their heat there- 4 to. The resulting spent and partially cooled reactivatinggases a're directed from reactor A1 through line 48 and valve 42 to zone C! which, in this case, serves as a cooler, whereby theV temperature ofthe gases is further reduced to the 'They then pass through line 3l and valve I8, together with regulated quantities of air admitted through line |42 and valve |43 into reactor A2, wherethrough the how is the same as that described in conjunction with revalve 84 to cooler actor A8' and wherefrom the partially cooled spent reactivating gases pass through line 32 and CI and thence through line 28 and valve 30, together with regulated quantities of air introduced through line |44 and valve |45 into reactor A'I. The ilow through reactor A| Vis the same as that described with reference to The spent and partially cooled reactivating gas stream is intimately contacted in scrubber with a spray of water or an aqueous solution of caustic soda or the like, to condense steam formed by combustion of the carbonaceous material in the catalyst beds and to remove any undesirable sulfur compounds and the like from the gases. The water or caustic solution is introduced to scrubber |5| through line |52 and valve |53, this line preferably terminating within the scrubber in a suitable spray head or the like indicated at |56. The spray material and condensed steam, containing the objectionable compounds removed from the combustion gases, are withdrawn from the lower portion of` the scrubber through line |54 and valve |55. The relatively cool combustion gases leaving scrubber |5| are directed through line |51 and valve |50 to compressor |59 by means of which they aresupplied through line |60 and valve |6| to heat exchanger |40, wherein they are partially reheated by passing therethrough in indirect heat exchange relation with the hot reactivating gases being returned, as previously described, to scrub'- ber |5I. vThe scrubbed and partially reheated gases are 'directed from heat exchanger |48,

- through line |62 and valve |63 into the combustion gas generator |30, wherein-they are commingled with controlled amounts of hot comalyst will have been completed and the .will serve nouseful purpose.

y 5 stream of gases entering reactor B2 through line |60 and valve |69, and line |10 containing valve `|'l| is provided for the introduction of controlled quantities of air into the streamvof reactivating gases entering reactor Bl. The spent reactivat- 4ing gases leaving reactor Bl pass through line |12 and valve |l|3 to line |46 wherefrom they pass, as previously described, to heat exchanger Md and thence to scrubber |5I.

At the end of each regenerating period, in case heat supplied from the hot products of regenerar,

tion to the mass of hot refractory material in the reactorawherein regeneration has been completed, is not suiilcient to fulill the heat requirements of the reactants passing through these -reactors in the subsequent processing period, the circulation of hot combustion gases from the combustion gas generator through these reactors back to the generator, in the manner above described, may be continued for a, suicient length of time to store therequiredadditional heat in During this period, when stream of combustion gases may be and is preferably discontinued since regeneration of the catadded air elevation of one 'speciilc form of reactor which bustion gases freshly lgenerated in this zone to form a mixture of combustion gases at substantially the temperature desired for reactivation of the catalyst. These gases are directed, as previ-- ously described, to the group of reactors wherein regeneration is taking place and controlled relatively small amounts of air are added to the stream of reactivating gases in' the manner previously described, prior to the initial and each successive contact of the gases lwith the catalytic material. The added air serves to support combustion oi the carbonaceous materials' deposited on the catalyst and the amount employed controls the rate of oxidation and the temperature attained inthe catalyst bed during regeneration. Since freshly generated hot combustion gases are' 'continuously added to the circulating stream of combustion gases employedas the oxygen-carrier and diluent, provision is made for vremoving .the excess of spent combustion gases from'the the meer.

When the catalyst beds inthe reactorsY of group `B are being reactivated,y the'ilow therethrough is the same as that'de'scribed in conjunction with 'the reactores! group A, with cooler C4 and C3 serving. respectively, t0 reduce the temperature of the reactivating gases passing from reactor may be employed in conducting the process oi the invention: The cylindrical outer shell |00 of the reactor is closed at the top and bottom by heads |0| and |02, respectively. A conduit '|03 is providedv in the top head which, in the case here illustrated, serves as an inlet line for ,reactants and. as an outlet line for spent reactlvatlng gases. A conduit |04 is provided in the bottom head which serves as an outlet line for reactants and/or concentric spaced screens or grids |05 and |06'v are provided in the central portionvof the shell and the space provided therebetween is substantially filled with catalyticmate'rial indicated at |01'. Thespace i0 enclosed by the inner cylindrical screen |05 is closed at the top by the member |09 which also closes ed the upper portion of the space in which the catalyst bed is disposed. Space |00 communicates at its lower end. with conduit |06. 'Ihe lower portion of the space containing the catalyst bed vis closed by member l. l0 and nozzle connections l or other suitable openings having removable cover plates ||2 and communicating with. the space provided between screens |05 and |06 in whichthe catalyst bed is.

disposed are provided inthe end members |00 and M0, these cover plates and openings being accessible through nozzles or other 'suitable openings H3 having removable cover plates H4 provided inthe top and bottom heads of the reactor;V whereby spent catalyst which isno longersuscepvtible to satisfactory reactivation may be removed [from the reactor, when required, and replaced -with fresh catalyst.

A concentric bed or mass 5 of refractory mafterial of relatively high heat capacity, such as checker-brlck work, glazed tile shapes, metallic members or the like. the bricks or other individual. members 'ofthe bed or mass preferably being of low porosity, is provided between the cylindrical Vouter wall |00 and the other cylindrical screen B3 to reactor B2 and from reactor B2 to reactor I A BI. Controlled'quantities of air are added to the |05 and is spaced from each to provide spaces H6 andV -therebetween. The outer space IIS is closed vat the bottom and open at .the top to communicate at its upper end with space l I8 provided between upper head and member |09, and the inner space II'I is closed at both ends.

A header or duct or conduit II9 communicating with conduit I 03 through line |20 having valve |2| disposed therein, is provided about the outer shell of the reactor and branch conduits |22 connect header I I9 directly with space Iii.

Valve |2| may be manually operated, but preferably is a variable ow type of automatic control valve actuated in response to the temperature of the materials within or leaving space I I'i by means of a thermostat or other temperature sensitive device 23 communicating with the valve through line |20. l

When conversion is taking place in the reactor of Fig. 2, the ow therethrough, as indicated by the arrows shown in solid lines, is as follows: .The stream of hydrocarbon vapors to be converted passes from conduit |00 into space H0. `The vapors flood space IIB between outer shell |00 and refractory mass I I5 and pass through the latter to space lil' between the refractory mass and the catalyst bed and are heated during their passage through the refractory mass by heat stored within the latter during a previous period of reactivation. 'Ihe heated vapors pass through screen |06 into and through the catalyst bed |01, wherein their conversion is accomplished and the resulting products pass through screen into space |08 wherefrom they are removed through conduit |04.

Due to the heat given up by the hot refractory mass to the hydrocarbon vapors passing therethrough, the temperature of said mass will de4 crease as the operation progresses and in order to maintain'the temperature of the heated hydrocarbon vapors entering the catalyst bed substantially constant. diminishing quantities of the vapors supplied to the reactor through conduit |03 by-pass the bed of hot refractory material by means of line |20, valve I2I, header IIS and lines |22. A small decrease in the temperature of the vapors entering the catalyst bed operates through the temperature sensitive device |23 to restrict the opening through valve I2I and send larger quantities of the vapors through the hot refractorymass. Thus, the temperature ofthe vapors the iiow through the reactor is reversed, as indicated by the arrows shown with broken lines, and oxygen-containing gases are directed through `entering the catalyst bed and the conversion to line |03 and thereby reduce the heat supplied' to the refractory mass. To permit this method of operation, a by-pass line |80 having control valve |8| disposed therein is provided around valve I2I, valve |2I remaining closed and valve |8|4 being regulated to suit requirements when regeneration is taking place in the reactor and valve I8I remaining closed while valve |26 is regulated to suit requirements while process of the reactants is taking place in the reactor.

As an example of one specific operation of the process herein provided, the charging stock is a Mid-Continent gas-oil of approximately 36 to 38 A. P. I. gravity and a synthetically prepared alumina-silica catalyst, containing approximately 15% alumina and approximately 85% silica and substantially free of alkali metal ions is employed. The charging stock is supplied to the system at the rate of approximately 1600 barrels (42 gallons) per stream day and the recycle ratio (ratio of recirculating reflux' condensate or recycle stock to raw oil is approximately 4:1, making a total of approximately 8000 barrels of combined feed subjected to cracking per stream day. -The combined feed is supplied through heater I5 from fractionator 0 at atemperature of approximately 720 F. and `is heated together with approximately 9500 pounds per hour offsteam toy an outlet temperature of approximately 950 F. with a superatmospheric pressure at the outlet of heater I6 of approximately 60 pounds per square inch. This quantity of steam gives a molecular ratio of steam to oil of approximately.1:l.

The stream of combined feedand steam is supplied from heater I5 at substantially the temperature and pressure mentioned to the first reactor of the series and in passing through the bed of hot refractory material in this zone is further heated to a temperature of approximately l975 F. at which temperature it enters the catalyst bed. The temperature of the oil vapors and steam leaving the first reactor is approximately 925 F. and this material is reheated in transit to the second reactor of the series to a temperature of approximately 950 F., further heated in passing through the bed of hot refractory material in this zone to a temperature of approximately 975 F. and then contacted with the second catalyst bed. The products leaving the second reactor ata temperature of approximately 925 F. are heated in ytransit to the third reactor to approximately line |04 to space I 08 wherefrom they pass through f screen |05 into and through the catalyst bed |01,

whereby carbonaceous material deposited during the previous processing cycle is burned from thecatalyst particles. The resulting hot gases pass through screen |06 into space IIIand thence through the refractory mass IIB to which they give upa substantial portion of their heat and wherefrom they are directed through space IIB and space ||8 to conduit |03 through which they are removed from the reactor. o v

In case the heat available from the hot reactivating gases leaving the catalyst hedv is substantially'more than that required by the reactants entering the catalyst bed in the subse'lquent processing period, the by-Pass arrange.- ment comp ing lines |22, header |I0 and line |20 may be employed to divert a regulated portion of the hot regenerating gases past vthe bed .ot refractory vmaterial in.. the reactor directly 950 F., further heated therein in passing through the bed'oi.' hot refractory material therein to a temperature of approximately 975 F., at which temperature they are contacted with the third bed of catalyst, emerging from the third reacrso tor of the series at a temperature of approxit mately 925 F. These products are cooled in heat exchanger I2 to a temperature of approximately 825 F. and introduced into separating chamber 5I which is operated at a superatmospheric pressure of approximately 30 pounds per square inch. Substantially the same pressure is employed in the succeeding fractionating, condensing and collecting equipment and stabilizerA 'I0 is operatedat a superatmospheric pressure of about 200 pounds per square inch. Fractionator I is operated with a top temperature regulated to give an overhead distillate product of approximately 450 F. end-boiling point.

The reactivating gases derived, as previously .I

desciabed, andl containing approximately 1.25% of free oxygen enter,y the iirst reactor of the series in which reactivation is taking` place at a temperature of approximately 925 F., are heated in passing through the catalyst bedA inthis zone to a temperature of approximately 1150 F. and, after giving up heat to the bed of refractory material through which they are then passed, emerge from this reactor at a temperature 0fl approximately 1025 F. They are then cooled in transit to the second reactor of the series to a temperature of approximately 950 F. and 'after suiiicient additional air is added thereto to bring.I the oxygen concentration back to that previously mentioned and the temperature to approximately of hot, oxygen-containing gases, heavy'carbon- 925 F. they are passed through the catalyst bed i in the second reactor, therein heated to a teniperature of approximately 1150 F., thence passed through the bed .ofrefractory material in this 'Zone and emerged from the second reactorat'a temperature of approximately 1025 F.' 'This procedure is repeated in the third reactor Aof the series 'after cooling the gases in Atransit thereto from the second reactor to a temperature 'of approximately 950 F. andrenewing their. oxygen concentration land the gases discharged from the third reactor` of theseries are cooled in the heat exchangerV to a temperature of approximately 950 F., the resulting cooled gases and about 5% of residual oil. Aside 'from the:v

small amount (approximately 4% by weight. of the charging oil) of coke deposited on the catf alyst and burned therefrom'during reactivation,

the remainderis chargeableto normally gaseous. fractions containing a high proportion of poly-i merizable olefins. Catalytic polymerization of fthe heavy olefinic components of these gases will yield an additional 12%, or thereabouts, based on the charging stock of polymer gasoline which may be blended with the catalyticaliy` cracked' product, giving an overall yield of 82% gas line having an octane number-(C. F.` R.) of 80 to82."' "1' v.

We claim'as our invention: 1..'Ihe processor catalytically cracking hy= drocarbon`pil, which comprises heating a flow' ing'stream of'saidoil to a temperature at which f.

it is `substantially 'completely vapor-ized under conditions regulated to preclude substantial ther- Vmal cracking thereonpassing the resulting ya porsin' series through a plurality oi' separate 'bedsof catalytic material and therein enacting '-said: catalytic. cracking, maintainingtemperain each bf. the; catalyst beds .within .the

range ',or conducting the' desired crack feetonfby'adiustig thel temperature Aof jsaid vaporsto the `desiredvali'ie ,prior to each successive Vcontact thereof-'with' a bedof .said f catalytic material,.-acc`omp lishing said" adjust- 'viously heated refractory material prior to their passage through each catalystbed of the series,

Y.. Vperiodically diverting the stream of va rs leav- I ying the iiijst mentionedtntcplto and "a ments atleast :in part, by `passing regulated -70 u quantities ofthe vapors through a mass of prethrough another group of separate catalyst beds in series and therein continuing the cracking reaction in the manner hereinbefore described, simultaneous with the passage of said vapor stream through the second group of catalyst beds, reactivating the catalyst in the iirst group of beds by burning from the catalyst, in a stream aceous materials deposited thereon 'during the cracking operation, utilizing resulting heated gases leaving each of the catalyst beds during' the reactivating step to supply heat to said refractry material for conducting a subsequent cracking step inthe same group of catalyst beds by-passing said heated gases in contact with said refractory material. subsequently again passing said stream. of hydrocarbon vapors from the irst mentioned heating step through the rst mentioned group of catalyst Ybedsftherein continuing the-cracking operation in the manner hereinbeiore described and reactivating the catalyst in the second mentioned group of beds in the same manner as hereinbefore described, directing conversion products throughout the operation from the group of catalyst beds wherein the cracking reaction is being conducted to sep'- arating and recovery equipment, therein separating from said productsmaterials boiling above -the range of the desired gasoline product and recovering the latter. A v

*2. The process dened in claim 1, wherein selected normally liquid fractions separated from said conversion products and boiling above the range of said gasoline are further cracked in the Y same system by supplying the same to the rst mentioned heating step.

3. The process defined in claim l, which includes the further steps of cooling the spentreactivating Bases leaving the group of catalyst beds wherein reactivation is taking place, removing a portion of the cooled gases from the system.' scrubbing the remaining portion thereof to remove deleterious components therefrom, re'- heating the scrubbed gases by passing the same in indirect v,heat exchange with the stream of lrelatively hot,. spent reactivating gases in the zone wherein said cooling of the latter is accomplished, further heating said scrubbed gases by commingling therewith freshly generated hot lcombustion gases in quantities substantially equivalent to the quantity of spent reactivating gas' removed rfrom the system, adding regulated minor amounts of air to the mixture and returning the same for further use as reactivating gases tothe group of catalystbeds wherein reactivation is taking place.A

- 4. In a' catalytic cracking process employing a reaction zone in which a stream oi' heated hydrocarbons tobe cracked is passed in contact with a bed of solid cracking catalyst and-wherein the cracking reaction is conducted, the supply of said hydrocarbons to the reaction zone being riodically discontinued whilewdeleterious heavy combustible .conversion products deposited in said bed during the cracking reaction are. burned therefrom to regenerate the lcatalyst by passing -relatively dilute hot oxidizing gases ln- .contact therewith,` the supply of said hydrocarbons to the reaction zone being subsequently renewed and thecracking' reaction therein continued, the improvement which comprises. during the regenerating step, passing hot gases leaving said catalyst bed in contact lwith a ot-refrectory material, ot high heat-capacity to store heat in thelatter and, during the sbsequentcracking contacting the heated refractory mass. com- 8 mingling said portions prior to their introduction into the catalyst bed, and diminishing the quantity of the second named portion as the cracking period progresses and as the hot refractory mass is cooled so as to maintain the temperature of 10 the commingled reactantsentering lthe catalyst bed substantially uniform during the entire cracking period.

5. In a catalytic cracking process employing a t reaction zone in which a stream of heated hylo drocarbons to be cracked is passed -in contact with a porous bed of solid cracking, catalyst of relatively lowrthermal conductivity and wherein the crackingn reactiomis conducted, the supply of said hydrocarbons to thereaction zone being periodically discontinued while deleterious heavy combustible conversion products deposited in said bed during the cracking reaction are burned therefrom to regenerate the catalyst by passing relatively dilute hot oxidizing gases in contact therewith, the supply of said hydrocarbons to the reaction zone being'subsequently renewed andthe cracking reaction therein continued, the improvement which comprises, during the regenerating step, passing a portion of the hot gases leaving the catalyst bed in .contact with a mass of refractory material of high heat capacity to store heat in the latter, preventing con-V tact between said mass and another portion of said hot gases, during the subsequent cracking 3 period passing hydrocarbon reactants tobe cracked in contactI with the heated refractory mass prior to their Icontact with the catalyst, whereby to supply to said reactants at least a to avoid excessive heat storage in the latter and assist in preventing excessive heating of the reactants passed therethrough during the subsequent cracking period. y 7. In a catalytic cracking process employing a plurality of reaction zones through which heated hydrocarbons to be cracked are passed in series ilow arrangement and contacted in each of said zones with a porous bed of solid cracking catalyst of relatively low thermal conductivity, the supply. of said hydrocarbons to the reaction zones being periodically discontinued while the catalyst disposed therein is regenerated by passing relatively dilute hot oxidizing gases in contact therewith -to burn from the bed comu bustible materials deposited therein during the cracking reaction, and the supply of said hydrocarbons to the reaction zones being subsequently rrenewed and their catalytic cracking therein continued, the improvement which comprises. during the regenerating period, passing hot regenerating gases leaving each of lsaid catalyst beds in contact with a mass of refractory material of high heat capacity to store heat in the latter and, during the subsequent cracking period, contacting hydrocarbons to be converted with thus head refractory material prior to each successive contact thereof with the catalyst. whereby to Supply to the hydrocarbons at least a portion of the heat required for effecting their catalytic cracking, the process being further characterized intthat the regenerating gases are passed through said reaction zones in series, the

portion of the heat required foreiecting said 40 eration ofthe Catalyst 1S accomplished Within a catalytic'cracking thereof, and so controlling the quantity of said hot gasesfnot passed in contact with said mass that substantially only the quantity of heat available in the hot gases which is i temperature range beneath that at which damage to the catalyst will occur. v 8. In a catalytic cracking process employing a plurality of reaction zones through which heatrequired for conducting the subsequent cracking l edhydrocarbons to be cracked are passed in operation is imparted to the refractory mass.

6. In a catalytic cracking process employing a' reaction zone inwhich-a stream of heated hy-k drocarbonsto be cracked is passed f.'-in contactv with a porous'bed oi' solid-.cra.ck ing .catalyst of -50 relativelyl low thermal conductivityv and wherein the cracking reaction is conducted, `the supply of said-hydrocarbons to the reaction, zone being periodicallyniscontinued while deleterious heavy combustible conversion products deposited in said bed dringthe cracking reactionvre burned f, thsrefrpm to regenerate the catalyst by passing relativelydilute hot oxidizing gases in contact therewith, the supply of said hydrocarbons to the reaction' zone being subsequently renewed and so 1 the cracking reaction therein continued, the im-Y provement whichl comprises,during' the regenerating step.' passing a portion of the hot gases leaving the catalyt bed in contact with a mass of refractory material of high heatl capacity to 65 contactwith the heated refractory mass prior to their contact.with the catalyst, whereby to supply t0 said reactants at least a portion of the heat required for Veffecting said catalytic cracking thereof, and limiting the quantity ofl said hot igasespassedgin contact refractorymass contact with said refractory material.

- series ow arrangement and contacted in each H,of said zones with a porous bedI of solid cracking catalyst of relatively low thermal conductivity,

the supply of said hydrocarbons tothe reaction zones being periodically discontinued while the catalyst disposed therein is regenerated by passing relatively dilute hot oxidizing gases in con'- tact therewithto burn from the` bed combustible materials deposited therein during the cracking reaction, and the supply of said hydrocarbons to the reaction zones being subsequently renewedl and their catalytic cracking therein continued, the improvement which comprises, during y,the

regenerating period, passing hot regenerating gases leaving each of said catalyst beds in' contact with a mass of refractory material vof high heat capacitytp store heat in the latter and, durv ing the subsequentcracking period, contactingl hydrocarbons to be converted. with thus heated refractory material prior to each successive contactv thereof with the catalyst, whereby to supply to the hydrocarbons a portion of the heat required foi-'effecting said catalytic cracking thereof, supplyingadditional heat to the hydrocarbons passing from each catalyst bed to the next sfuccessive catalyst bed, and abstracting heat from the hot reactivating gases passing from each catalyst bed to the next successive catalyst bed, in additionto that abstracted therefrom by their 9. In a conversion process wherein heat is periodically stored in a mass of refractory material, reactants tobe converted being passed, subsequent to said heating of the mass, in contact therewith to abstract heat therefrom and supply heat to the reactants, the thus heated reactants being subsequently supplied to a Zone wherein the desired conversion thereof is eiected, the improvement which comprises, passing only a portion of the total reactants being supplied to said conversion zone in contact with said hot refractory mass, commingling the remaining portion thereof with the'heated reactants discharged from said mass, supplying the commingled reactants to said conversion zone, and increasing the quantity of the rst named portion as the operation progresses and as the hot refractory mass is cooled to maintain the temperature of the commingled reactants being supplied to said conversion zone substantially con stant.

10. In a conversion process employing a re-v action zone wherein hydrocarbon reactants to be converted are contacted with a porous bed of solid contact material which promotes their endothermic conversion, the supply of` said reactants to the reaction zone being periodically discontinued while deleterious heavy combustible conversion products deposited in said bed during the conversion reaction are burned therefrom to regenerate the same by passing relatively dilute hot oxidizing gases in contact therewith, the supply `of said reactants to the reaction zone being subsequently renewed and the conversionreaction therein continued, the improvement which comprises, during the regenerating step, passing hot gases leaving said bed in contact with a mass of refractory material of high heat capacity to during the subsequent conversion period passing hydrocarbon reactants to be converted in contact with the heated refractory mass prior to their contact withsaid bed, whereby to supply to said reactants at least a portion of the heat required for effecting their conversion, and so controlling `the quantity of said hot gases notpassed in contactl with said mass that substantially only the lquantity of heat available inthe hot gases which is required for conducting the subsequent conj version step is imparted to the refractory mass.

12. In a conversion process employing a reac` tion zone wherein hydrocarbon reactants to be converted are contacted with a porous bed of store heat in the latter and, during the subsen quent conversion period, passing a regulated quantity of the hydrocarbon reactants to be converted in contact with said heated refractory mass to supply 4heat to the reactants, commingling the thus heated reactants with another regulated quantity of said hydrocarbon react. ants not contacted with the hot refractory mass, passing the commingled reactants into contact with said bed, and diminishing the quantity of reactants not passed in contact with said hot refractory mass as the conversion period progresses and as the hot refractory mass is cooled so as to maintain the temperature of the commingled reactants entering said bed substantially uniform during the. entire conversion period.

11. In a conversion process employing a reaction zone wherein hydrocarbon reactants to be converted are contacted with a porous bed oi' solid contact material which promotes endothermic conversion of the reactants, the supply of said hydrocarbons to the reaction zone being periodically discontinued while deleterious heavy combustible conversion, products depositedv in said .bed during the conversion reaction are burned therefrom to regenerate the same by Passing relatively dilute hot oxidizing gases in contact therewith, the supply of said reactants to the reaction zone being subsequently renewed and the conversion reaction threin continued,

`the improvement which comprises, during the regenerating step passing a portion of the hot gases leaving said bed in contact with a mass of refractory material of high heat capacity to store heat in the latter, preventing contact between said mass and another portion of said hot gases,

solid contact material which promotes endothermic conversion of the reactants, the supply of said hydrocarbons to the reaction zone being periodically discontinued while deleterious heavy combustible conversion products deposited in said bed during the conversion reaction are burned therefrom to regenerate the same by passing relatively dilute hot oxidizing gases in contact therewith, the supply of said-reactants to the reaction zone being subseuqently renewed and the conversion reaction therein continued, the improvement which comprises, during the regenerating step passing a portion of the hot gases leaving said bed in contact with a mass of refractory material of high heat capacity to store heat in the latter, preventing contact between said mass and another portion of said hot gases, during the subsequent conversion vperiod passing hydrocarbon reactants to be converted in contact with the heated refractory mass prior to their contact with said bed, whereby to supply to said reactants at least a portion of the -heat required for eifecting their conversion, and limiting the quantity of said hot gases passed in contact with the refractory mass to avoid excessive heat storage in the latter and assist in preventing excessive heating of the reactants passed therethrough during the subsequent conversion period.

i 13. In a conversion process employing a pluralityof reaction zones through which heated hy.. drocarbon reactants to be converted are passed in series flow arrangement and contacted in each of said zones with a porous bed of solid contact material of relatively low thermal conductivity which promotes their endothermic conversion, the supply of `said reactants to the reaction zones being periodically discontinued while the contact material disposed therein is regenerated by passing relatively dilute hot oxidizing gases in contact therewith to burn from the bed combustible materials deposited therein during the conversion reaction, and the supply of said reactp ants to said reaction zonesbeing subsequently renewed and their endothermic conversion therein continued, the improvement which comprises, during the regenerating period, passing hot regenerating gases leaving each of said beds in contact with a mass of refractory material of high heat capacity to store heat in the latter and, during the subsequent conversion -period contacting reactants to be converted with thus heated refractory material prior to each successive contact thereof with the contact material, whereby to supply to said reactants at least a portion ofthe heat required for effecting said conversion thereof, the process being furtherA characterized in that the regenerating gases are passed through said reaction zones in series, the

temperature of the reactivating gases passing from the hot refractory material to each successivc bed of contact material being so modined and the oxygen concentrationof the reactivating gases entering each bed of contact material and their rate of now therethrough being so maintained that regeneration of the contact beds is accomplished within a temperature range beneath that at which damage to the contact material willoccur.

14. In a conversion process employing a pluassumes 15. The process of catalytically converting hy. drocarbons, which comprises heating a flowing stream thereof tg the desired conversion temperature under conditions regulated to preclude substantial thermal conversion thereof, 'passing resulting heated reactants in series through sep- A arate beds of active catalytic material and thererality of reaction zones through which heated hydrocarbon reactants to b e converted are passed in series flow arrangement and contacted in each of said zones with a porous bed of solid contact material` of relatively lomthermal conductivity which promotes their endothermic conversion, the supply of said reactai'its-l to the reaction zones being periodically discontinued while the contact material disposed therein is regenerated by passing relatively dilute hot oxidizing gases in contact therewith to burn from the bed combustible materials deposited therein during the conversion reaction, and the supply of said reactants to said reaction zones being subsequently renewed and their endothermic conversion therein continued, the improvement which comprises, .during the regenerating period,v passing hot regenerating gases leaving each of said beds in contact with a mass of refractory. material of high heat capacity to store heat in the latter and, during the subsequent conversion period contactingy reactants to be converted withthusheated refractory material prior to each successive contact thereof with the .contact material, whereby tov supply to said reactants a portion of the heat required for effecting said endothermicconversion thereof, supplying additional heat to the reactants passing from each bed of contact material to the next successive bed thereof, and abstracting heat from the reactivating gases passing from each bed of contact material to the next successive bed thereof, in addition to that abstracted therefrom4 by their contact with said refractory material.

Iis

in effecting said catalytic conversion thereof, maintaining the temperature in each of said catalyst beds within the range required for conducting the desired conversion reaction by adjusting the temperature of said reactants to the desired value prior to each successive contact thereof with'a bed of said catalytic material, accomplishing said adjustment, at least in part, by

' passing said reactants in regulated quantity through a mass of previously heated refractory material prior to each successive contact thereof with the catalyst, periodically diverting said stream of reactants to and through another group of separate catalyst-beds in series and therein continuing the conversion reaction in the manner hereinbefore described, simultaneous with the passage of said heated reactants through the second group of catalyst beds, regenerating'the catalyst in the first group of beds by burning therefrom heavy combustible conversion products deposited thereon during the preceding conversion reaction in a stream of hot oxidizing gases, utilizing resulting hot regenerating gases leaving each of the catalyst beds during the regenerating step to supply heat to said refractory material i'or conducting the subsequent conversion step in the same group of catalyst beds by passing hot gases thus derived in contact with the refractory material, subsequently again passing said stream of hydrocarbon reactants in contact with the catalyst beds of the first mentioned lgroup and therein continuing the conversion reaction 40 in the same manner as hereinbefore described.

PERCY summa Lnv A. Mamma. 

